Method and system for preparing caprolactam

ABSTRACT

The present disclosure provides a method for preparing a caprolactam and the method includes steps of subjecting cyclohexanone oxime and sulfuric acid to a Beckmann rearrangement reaction to obtain a rearrangement mixture; neutralizing the rearrangement mixture and extracting the neutralized rearrangement mixture using an organic solvent sequentially; and subjecting the extracted organic solution to a hydrogenation reaction so as to simplify the process to produce a high quality caprolactam.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a divisional of U.S. application Ser. No.14/996,723, filed Jan. 15, 2016, which claims under 35 U.S.C. § 119(a)the benefit of Taiwanese Patent Application No. 104104987 filed Feb. 13,2015, the entire contents of which are incorporated herein by reference.

BACKGROUND

1. Technical Field

The present disclosure relates a method for preparing caprolactam, andmore particularly to a method for preparing caprolactam with asimplified process.

2. Description of Related Art

Caprolactam is an important raw material for the production of nylon 6fibers and resins. In order to produce high quality caprolactam tosatisfy the production of Nylon-6 or polymerization of the resin, thereare many purification steps in the traditional production process. Thesepurification steps comprise an organic solvent extraction, alkalinewashing, back-extraction of caprolactam solution with water(water-back-extraction), steam stripping of removing organic solvent,ion exchange, and hydrogenation reactions, and finally the process iscompleted with evaporation and distillation steps to produce a highquality caprolactam. For example, to produce caprolactam in theindustry, U.S. Pat. No. 7,700,767 discloses, under the oleum-catalyzedcondition, cyclohexanone oxime was subjected to Beckmann rearrangementreaction, then the reaction mixture was neutralized with ammonia andsubsequently was subjected to solvent extraction with benzene. Theorganic phase portion of benzene was collected, then undergone alkalinewashing and water-back-extraction. Benzene was removed by steamstripping to obtain an aqueous solution of caprolactam with aconcentration of about 30 to 40 wt %. The process was followed by ionexchange treatment system to remove inorganic salt impurities incaprolactam aqueous solution. Later, with the presence of hydrogen and anickel-containing catalyst, unsaturated organic impurities in thecaprolactam aqueous solution was reacted with hydrogen. Finally, thecaprolactam solution was evaporated and distillated to obtaincaprolactam products.

European Patent No. 411,455 discloses a continuous caprolactampurification method using cyclohexanone oxime subjected to Beckmannrearrangement, neutralization with ammonia, solvent extraction ofbenzene, steam stripping to remove the organic solvent, and othertraditional manufacturing processes, and finally an aqueous solutionform of caprolactam was subjected to the three-phase(vapor-liquid-solid) hydrogenation fixed bed operating system. Inaddition, U.S. Pat. No. 5,539,106 discloses a hydrogenation purificationmethod for a caprolactam-water mixture, in which the caprolactam-watermixture is first contacted with the gaseous hydrogen, followed bycontacting a hydrogenation catalyst for hydrogenation purification in afixed bed.

It can be seen that, in the existing hydrogenation steps of thecaprolactam manufacturing method, an aqueous solution of caprolactam isused for the reaction. Therefore, the steps of water-back-extraction arenecessary to remove organic solvents in the aqueous solution. Itconsumes large amounts of steam energy. Moreover, ion exchange stepwhich is carried out prior to the hydrogenation reaction in conventionalmanufacturing process requires frequent replacement and regeneration ofion exchange resins with increased production cost and the subsequentwaste-water treatment problems.

Therefore, how to simplify the manufacturing process to producehigh-quality caprolactam has become the issue to be resolved anxiously.

SUMMARY

The present disclosure provides a method for preparing caprolactam thatperforms a hydrogenation reaction using an organic solution containingcaprolactam. In addition, in the preparation method of the presentdisclosure, after cyclohexanone oxime and sulfuric acid are subjected toa Beckmann rearrangement reaction to obtain a rearrangement mixture, itis adequate to merely perform neutralization reaction, organic solventextraction and alkaline washing prior to performing the hydrogenationreaction using an organic solution containing caprolactam. In oneembodiment, the caprolactam organic solution is treated by evaporationand distillation to obtain caprolactam products. As compared to existingprior art, the traditional steps of water-back-extraction and ionexchange are simplified to reduce a large amount of steam consumptionsand to resolve the subsequent waste-water treatment problems. Thesimplified method for preparing caprolactam of the present disclosurecan produce high-purity caprolactam.

In one embodiment, the present disclosure provides a method forpreparing caprolactam comprising steps of:

-   -   (a) subjecting cyclohexanone oxime and sulfuric acid to a        Beckmann rearrangement reaction to obtain a rearrangement        mixture;    -   (b) neutralizing the rearrangement mixture with an alkali to        obtain a first crude caprolactam solution rich in caprolactam        and a second crude caprolactam solution rich in sulfate;    -   (c) extracting at least the first crude caprolactam solution        with an organic solvent to obtain a caprolactam organic        solution;    -   (d) mixing the caprolactam organic solution with hydrogen to        perform a hydrogenation reaction in a hydrogenation reactor        having a hydrogenation catalyst, wherein a weight hourly space        velocity (WSHV) of the caprolactam organic solution is 1 to 20        per hour, a feeding hydrogen flow rate is 0.01 to 0.15 NM³ per        hour per cubic meter of the caprolactam organic solution, and a        hydrogen gauge pressure of an outlet of the hydrogenation        reactor is 3 to 20 kg/cm²; and    -   (e) purifying the hydrogenated caprolactam organic solution.

In one embodiment, the method for preparing caprolactam of the presentdisclosure further comprises extracting the second crude caprolactamsolution with the organic solvent to obtain the caprolactam organicsolution. The organic solvent can be used to extract the first crudecaprolactam solution and the second crude caprolactam solution at thesame time, or to extract the first crude caprolactam solution and thesecond crude caprolactam solution, respectively.

In one embodiment, the organic solvent for extraction in the presentdisclosure is an aromatic hydrocarbon or a halogenated hydrocarbon.

In another embodiment, the organic solvent for extraction in the presentdisclosure is toluene, benzene or dichloroethane.

In one embodiment, the alkali for the neutralization reaction in thepresent disclosure is ammonia.

In one embodiment, the method for preparing caprolactam of the presentdisclosure further comprises adjusting the electric conductivity of thecaprolactam organic solution to 5 to 100 μmoh/cm with an alkali aqueoussolution after the step (c).

In still another embodiment, the method for preparing caprolactam of thepresent disclosure further comprises removing at least a portion of theorganic solvent after the step (c).

In one embodiment, the hydrogenation catalyst for the hydrogenationreaction of the present disclosure comprises a carrier and an activemetal carried on the carrier, wherein the carrier is one selected fromthe group consisting of alumina, carbon and silica.

In one embodiment, the active metal is one selected from the groupconsisting of ruthenium, rhodium, palladium, platinum and nickel.Further, an amount of the active metal is 5 to 85 wt %.

In one embodiment, an amount of the nickel is 5 to 85 wt %.

In one embodiment, the reaction temperature of the hydrogenationreaction of the present disclosure is 50 to 180° C.

In one embodiment, the method for preparing caprolactam of the presentdisclosure further comprises adding at least one alkali metal hydroxidein the hydrogenated caprolactam organic solution, prior to or during thestep (e).

The present disclosure further provides a system for preparingcaprolactam comprising: a reaction unit configured to subjectcyclohexanone oxime and sulfuric acid to a Beckmann rearrangementreaction to obtain a rearrangement mixture; a neutralization unitconnected with the reaction unit and configured to receive therearrangement mixture from the reaction unit, wherein the neutralizationunit contains an alkali to perform a neutralization reaction with therearrangement mixture to obtain a first crude caprolactam solution richin caprolactam and a second crude caprolactam solution rich in sulfate;an extraction unit connected to the neutralization unit and configuredto receive at least the first crude caprolactam solution from theneutralization unit, wherein the extraction unit contains an organicsolvent to extract at least the first crude caprolactam solution toobtain a caprolactam organic solution; a hydrogenation unit connected tothe extraction unit and configured to receive the caprolactam organicsolution from the extraction unit, wherein the hydrogenation unitcomprises hydrogen and a fixed bed, and a hydrogenation catalyst isdisposed on the fixed bed to subject the caprolactam organic solutionand hydrogen to a hydrogenation reaction, and wherein a weight hourlyspace velocity (WSHV) of the caprolactam organic solution is 1 to 20 perhour, a feeding hydrogen flow rate is 0.01 to 0.15 NM³ per hour percubic meter of the caprolactam organic solution, and a hydrogen gaugepressure of an outlet of the hydrogenation reaction is 3 to 20 kg/cm²;and a purification unit connected to the hydrogenation unit andconfigured to receive the hydrogenated caprolactam organic solution fromthe hydrogenation unit, wherein the purification unit comprises anevaporation device and a distillation device.

In one embodiment, the system for preparing caprolactam of the presentdisclosure further comprises a first temporary storage unit connectedwith the extraction unit and the hydrogenation unit, and configured toreceive the caprolactam organic solution from the extraction unit,wherein the electric conductivity of the caprolactam organic solution isadjusted to 5 to 100 μmoh/cm with an alkali aqueous solution.

In another embodiment, the system for preparing caprolactam of thepresent disclosure further comprises a first concentration unitconnected with the extraction unit and the hydrogenation unit, andconfigured to receive the caprolactam organic solution from theextraction unit, with at least a portion of the organic solvent beingremoved.

In another embodiment, the system for preparing caprolactam of thepresent disclosure further comprises a second temporary storage unit anda second concentration unit connected with the temporary storage unit,and the temporary storage unit, wherein the second temporary storageunit and the second concentration unit are disposed sequentially afterthe extraction unit, and wherein the concentration unit is connectedwith the hydrogenation unit.

Further, in one embodiment, the system for preparing caprolactam of thepresent disclosure further comprises a third temporary storage unitconnected with the hydrogenation unit and the purification unit toreceive the hydrogenated caprolactam organic solution from thehydrogenation unit, with at least one alkali metal hydroxide added tothe hydrogenated caprolactam organic solution.

It can be realized from the above that the method and system thereof forpreparing caprolactam of the present disclosure is based on a novelhydrogenation method by eliminating the steps of water-back-extraction,solvent steam stripping, and ion exchange treatment in the conventionalprocesses. It reduces energy consumptions of the steam stripping andusage of aqueous solution. It also does not require to replace ionexchange resins without increasing the cost for the subsequentwaste-water treatment. Compared to the lengthy steps of the conventionalprocesses associated with the issues of significant consumption of steamenergy, the method for preparing caprolactam and system thereof of thepresent disclosure not only produce a high quality of caprolactam, butalso have advantages of energy-saving and simplified process.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic diagram illustrating the system for preparingcaprolactam.

FIG. 2 is a schematic diagram illustrating the extraction units of thesystem for preparing caprolactam in parallel-connection extraction.

FIG. 3 is a schematic diagram illustrating the system for preparingcaprolactam that further comprises a temporary storage unit.

FIG. 4 is a schematic diagram illustrating the system for preparingcaprolactam that further comprises a concentration unit.

FIG. 5 is a schematic diagram illustrating the system for preparingcaprolactam that further comprises a temporary storage unit and aconcentration unit.

FIG. 6 is a schematic diagram illustrating the system for preparingcaprolactam that further comprises a temporary storage unit according toanother embodiment.

FIG. 7 is a schematic diagram illustrating the system for preparingcaprolactam that further comprises a temporary storage unit according tostill another embodiment.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The following specific examples are used for illustrating the presentdisclosure. A person skilled in the art can easily conceive the otheradvantages and effects of the present disclosure based on the disclosureof this specification.

The present disclosure provides a method for preparing caprolactamcomprising the following steps:

-   -   (a) subjecting cyclohexanone oxime and sulfuric acid to a        Beckmann rearrangement reaction to obtain a rearrangement        mixture;    -   (b) neutralizing the rearrangement mixture with an alkali to        obtain a first crude caprolactam solution rich in caprolactam        and a second crude caprolactam solution rich in sulfate;    -   (c) extracting at least the first crude caprolactam solution        with an organic solvent to obtain a caprolactam organic        solution;    -   (d) mixing the caprolactam organic solution with hydrogen to        perform a hydrogenation reaction in a hydrogenation reactor        having a hydrogenation catalyst, wherein a weight hourly space        velocity of the caprolactam organic solution is 1 to 20 per        hour, a feeding hydrogen flow rate is 0.01 to 0.15 NM³ per hour        per cubic meter of the caprolactam organic solution, and a        hydrogen gauge pressure of an outlet of the hydrogenation        reactor is 3 to 20 kg/cm²; and    -   (e) purifying the hydrogenated caprolactam organic solution.

To implement the method for preparing caprolactam of the presentdisclosure, the present disclosure further provides a system forpreparing caprolactam comprising a reaction unit, a neutralization unit,an extraction unit, a hydrogenation unit and a purification unit.

As shown in FIG. 1, it is a schematic diagram illustrating the systemfor preparing caprolactam of the present disclosure. The systemcomprises a reaction unit 101; a neutralization unit 102 which isconnected to the reaction unit 101 via a pipe 108 a, wherein theneutralization unit 102 is connected with additional pipe 108 b; anextraction unit 103 which is connected to the neutralization unit 102via a pipe 109; a hydrogenation unit 104 which is connected to theextraction unit 103 via a pipe 110; and a purification unit 105 which isconnected to the hydrogenation unit 104 via a pipe 111.

According to the above system for preparing caprolactam, thehydrogenation unit 104 has a fixed bed 112, and a hydrogenation catalyst(not shown) is fixed on the fixed bed 112. Further, the purificationunit 105 comprises an evaporation device 106 and a distillation device107.

Moreover, in one example, the evaporation device 106 can be selectedfrom a multi-effect evaporation device or a vapor re-compressionevaporation device. The distillation device 107 can be commonly useddistillation column, and the evaporation device 106 is connected withthe distillation device 107 via a pipe 113.

In the step (a), according to the conventional art, the cyclohexanoneoxime is subjected to a Beckmann rearrangement reaction in the reactionunit 101 under the catalysis of sulfuric acid to produce a rearrangementmixture.

Then, the rearrangement mixture is fed from the reaction unit 101 intothe neutralization unit 102 via the pipe 108 a. In the step (b), thepipe 108 b delivers an alkali to the neutralization unit 102 whichallows the alkali and the rearrangement mixture to perform aneutralization reaction to obtain a first crude caprolactam solutionrich in caprolactam and a second crude caprolactam solution rich insulfate, wherein the commonly used alkali is ammonia and the obtainedsulfate is ammonium sulfate accordingly. The neutralization reactionwith the usage of ammonia allows the formation of ammonium sulfatederived from sulfuric acid. After completion of the neutralizationreaction, it allows the formation of the first crude caprolactamsolution rich in caprolactam in the upper layer and the formation of thesecond crude caprolactam solution rich in sulfate with small amount ofcaprolactam in the under layer. The term “first crude caprolactamsolution rich in caprolactam” as used herein refers that the amount ofcaprolactam is more than 50 wt %. The term “second crude caprolactamsolution rich in sulfate” as used herein refers that the amount ofsulfate is more than that of caprolactam. Further, the amount ofcaprolactam in the first crude caprolactam solution rich in caprolactamis about 68 to 75 wt %, in which there are additional organic andinorganic impurities. The pH value of the aqueous solution is 4.0 to6.0.

In the step (c), the first crude caprolactam solution is extracted atleast with the organic solvent to obtain the caprolactam organicsolution. As shown in FIG. 1, the extraction unit 103 is connected tothe neutralization unit 102, and the pipe 109 receives the first crudecaprolactam solution fed from the neutralization unit 102, and theextraction unit 103 has the organic solvent so as to extract at leastthe first crude caprolactam solution to obtain the caprolactam organicsolution.

In one embodiment, the method for preparing caprolactam of the presentdisclosure further comprises a step of extracting the second crudecaprolactam solution with the organic solvent to obtain a secondcaprolactam organic solution. The organic solvent can simultaneouslyextract the first crude caprolactam solution and the second crudecaprolactam solution in series mode or in parallel mode. Also as shownin FIG. 2, the extraction unit 103 has chambers 114 and 115 forextracting the first crude caprolactam solution and the second crudecaprolactam solution in parallel mode, respectively.

According to the above step (c), the extraction unit 103 used for theextraction is not particularly limited. The examples of the extractionunit 103 include, but not limited to, at least one selected from thegroup consisting of packed column, plate column, pulse column, rotarydisc column and vibratory column.

According to the above method, the organic solvent used for theextraction is not particularly limited. The examples of the organicsolvent include, but not limited to, at least one selected from thegroup consisting of toluene, benzene and ethylene dichloride.

In one embodiment, the method for preparing caprolactam of the presentdisclosure further comprises a step of adjusting the electricconductivity of the caprolactam organic solution with water or anaqueous solution containing an alkali after the step (c) and prior tothe hydrogenation. The electric conductivity is controlled at 5 to 100μmoh/cm, preferably 5 to 40 μmoh/cm. The usage of water or the aqueoussolution containing the alkali is 0.01 to 0.5 times of the volume ofcaprolactam organic solution, preferably 0.01 to 0.1 times of the volumeof caprolactam organic solution, wherein the examples of the alkalineaqueous solution are not particularly limited. The example of thealkaline aqueous solution includes a solution of an alkali metal, suchas sodium hydroxide solution.

According to the above embodiment, as the aspect shown in FIG. 3, it iscorresponding to the system for preparing caprolactam of the presentdisclosure. The system for preparing caprolactam further comprises atemporary storage unit 116, which is connected with the extraction unit103 and the hydrogenation unit 104, and the pipe 117 receives thecaprolactam organic solution fed from the extraction unit 103, and thenthe caprolactam organic solution with adjusted electric conductivity isdischarged into the hydrogenation unit 104 via the pipe 118.

In still one embodiment, the method for preparing caprolactam of thepresent disclosure further comprises a step of removing at least aportion of the organic solvent after the step (c). As the aspect shownin FIG. 4, the system for preparing caprolactam further comprises aconcentration unit 119, which is connected with the extraction unit 103and the hydrogenation unit 104, and the caprolactam organic solution fedfrom the extraction unit 103 is received via the pipe 120, and then theconcentrated caprolactam organic solution is fed into the hydrogenationunit 104 via the pipe 121. The system for preparing caprolactam of thepresent disclosure is not limited to the above embodiments. The systemfor preparing caprolactam of the present disclosure can further comprisethe temporary storage unit 116 and the concentration unit 119 at thesame time, and the extraction unit 103 can be selected from the seriesextraction or the parallel extraction with the chambers 114 and 115without particular limitation. As the aspect shown in FIG. 5, the systemfor preparing caprolactam of the present disclosure comprises thetemporary storage unit 116 and the concentration unit 119 connected withthe temporary storage unit 116, and the temporary storage unit 116 andthe concentration unit 119 are disposed sequentially after theextraction unit 103, and the concentration unit 119 is connected withthe hydrogenation unit 104, wherein the temporary storage unit 116receives the caprolactam organic solution fed from the extraction unit103 via the pipe 122, and the concentration unit 119 receives thecaprolactam organic solution fed from the temporary storage unit 116 viathe pipe 123, and the concentrated caprolactam organic solution is fedinto the hydrogenation unit 104 via the pipe 124.

In the present disclosure, the steps of water-back-extraction, solventsteam stripping, and ion exchange treatment in the conventional processare eliminated. In the step (d), the hydrogenation of the extractedcaprolactam organic solution is directly performed with hydrogen,wherein, as the aspect shown in FIG. 1, the hydrogenation unit 104 usedfor the hydrogenation is connected to the extraction unit 103 via thepipe 110, and the caprolactam organic solution in the extraction unit103 is received via the pipe 110, and the hydrogenation catalyst isfixed on the fixed bed 112 of the hydrogenation unit 104.

In one embodiment, the hydrogenation unit 104 is not particularlylimited and can be selected from a trickle-bed reactor and a bubblingreactor.

In the step (d), as mentioned above, the concentration of the extractedcaprolactam organic solution used in the present disclosure is notparticularly limited. The concentration unit 119 can be optionally usedfor removing the organic solvent to increase the concentration of thecaprolactam organic solution. The concentration of the caprolactamorganic solution is preferably 10 to 80 wt %.

In one example, a weight hourly space velocity of the caprolactamorganic solution is 1 to 20 per hour, more preferably 1 to 15 per hour.

In one embodiment, a feeding hydrogen flow rate is 0.01 to 0.15 NM³ perhour per cubic meter of the caprolactam organic solution, and a hydrogengauge pressure of an outlet of the hydrogenation reactor is 3 to 20kg/cm².

The hydrogenation catalyst of the present disclosure is consisting of ametal and a carrier. In one embodiment, the carrier of the hydrogenationcatalyst is one selected from the group consisting of alumina, carbonand silica. The metal of the hydrogenation catalyst is one selected fromthe group consisting of ruthenium, rhodium, palladium, platinum andnickel. The metal amount of the hydrogenation catalyst is 5 to 85 wt %,more preferably 15 to 60 wt %.

In one example, the nickel amount of the hydrogenation catalyst is 5 to85 wt %.

In one embodiment, temperature of the hydrogenation of the presentdisclosure is 50 to 180° C., preferably 50 to 150° C., more preferably80 to 120° C.

After that, in the step (e), the hydrogenated caprolactam organicsolution is purified, wherein the purification includes steps ofevaporation and distillation to separate the caprolactam. The evaporatedorganic solution can be recovered to a solvent recovery system forrecycling. As the aspect shown in FIG. 1, the purification unit 105 usedfor the purification is connected to the hydrogenation unit 104 via thepipe 111, and the caprolactam organic solution in the hydrogenation unit104 is fed into the purification unit 105 via the pipe 111.

In one example, the purification unit 105 comprises the evaporationdevice 106 and the distillation device 107. Further, the evaporationdevice 106 can be selected from a multi-effect evaporation device or avapor re-compression evaporation device. The distillation device 107 canbe a commonly used distillation column.

In the step (e), the distillation step of the purification is operatedat less than 50 mmHg vacuum levels, preferably 20 mmHg, and morepreferably 10 mmHg. The temperature of the bottom of the boiler is setat 100 to 220° C., preferably 100 to 180° C., more preferably 100 to150° C. For the distillation, light impurities with the boiling pointless than the caprolactam initially are distilled under a low degree ofvacuum, while the caprolactam is distilled under a higher degree ofvacuum. The remaining residues at the bottom of the distillation unitare ionic impurities, amino acid alkali salts, organic impurities with ahigh boiling point, and etc.

In one embodiment, at least one of alkali metal hydroxide can be furtheradded into the hydrogenated caprolactam organic solution prior to thepurification or during the purification, such that helps to reduce theaggregation phenomena occurred during the distillation process and toenable a portion of impurities in the solution to form the amino acidsalts which can be easily removed from the distillation system.

According to the above examples, as the aspect shown in FIG. 6, thesystem for preparing caprolactam of the present disclosure furthercomprises a temporary storage unit 125 which is connected to thehydrogenation unit 104 via the pipe 126, and the caprolactam organicsolution in the hydrogenation unit 104 is fed via the pipe 126, and thenthe caprolactam organic solution is fed into the purification 105 viathe pipe 127.

In another aspect, as the aspect shown in FIG. 7, the system forpreparing caprolactam of the present disclosure further comprises atemporary storage unit 128 which is connected to the purification unit105 via the pipe 129, and at least one of alkali metal hydroxide isadded via the pipe 129.

The system for preparing caprolactam of the present disclosure is notlimited to the above examples. The temporary storage unit 125 of FIG. 6or the temporary storage unit 128 of FIG. 7 can be present in the systemfor preparing caprolactam with the temporary storage unit 116 of FIG. 3or the concentration unit 119 of FIG. 4 at the same time. Also, thesystem can comprise the temporary storage unit 116 and the concentrationunit 119 at the same time, and also are present with the temporarystorage unit 125 or the temporary storage unit 128 simultaneously. It isnot particularly limited.

At the same time, the extraction unit 103 can be selected from theseries extraction or the parallel extraction with the chambers 114 and115, and it is not particularly limited.

According to the above examples, the alkali metal hydroxide is at leastone selected from the group consisting of sodium hydroxide and potassiumhydroxide, preferably sodium hydroxide. The amount of the alkali metalhydroxide is no more than 20 milliequivalent/per kilogram of thecaprolactam organic solution, preferably 1 to 10 milliequivalent/perkilogram of the caprolactam organic solution.

EXAMPLES

According to the aforementioned conventional manufacturing process,cyclohexanone oxime and sulfuric acid were subjected to a Beckmannrearrangement reaction, and then followed by neutralization reactionwith ammonia. Then the aqueous solution rich in crude caprolactam andammonium sulfate solution containing small amounts of caprolactam werepumped into the extraction column, respectively, and contacted withbenzene solvent. Two streams of caprolactam organic solutions werebrought together, and washed with alkali and water. The conductivity ofthe caprolactam organic solution after washing was 54 μmoh/cm, acaprolactam benzene solution with a concentration of 25.3 wt % wasobtained, and the caprolactam benzene solution contained 1.25 wt % ofwater. This caprolactam benzene solution was used as the source of thecaprolactam organic solution for the following examples and comparativeexamples to carry out the subsequent steps.

Example 1

The caprolactam benzene solution with a concentration of 25.3 wt % wasintroduced to the hydrogenation reactor with a fluid dispenser on thetop by a quantitative pump. A hydrogenation catalyst containing nickelwas fixed on the fixed bed, and the nickel amount was 40 wt %. Theweight hourly space velocity of the caprolactam benzene solution was setto 4.0 per hour, while a hydrogen gauge pressure of an outlet of thehydrogenation reactor was set to 5.5 kg/cm², and the feeding hydrogenflow rate was set to less than 0.05 NM³ per hour per cubic meter of thecaprolactam benzene solution, and the hydrogenation temperature was setto 90° C.

Next, sodium hydroxide was added to the hydrogenated caprolactam benzenesolution that was equivalent to 8 mEq of sodium hydroxide per kg ofcaprolactam benzene solution. It was followed by solvent concentrationtreatment using concentrating machine with reduced pressure. The lightimpurities were removed by distillation with a degree of vacuum of 10 to15 mmHg. Finally, caprolactam was distilled with high level of vacuum of3 to 10 mmHg. The volatile alkali, alkalinity, potassium permanganatenumber (PM), potassium permanganate absorption number (PAN), extinctionvalue, and chroma of the distilled caprolactam were measured andrecorded in Table 1.

Example 2

The procedure of example 1 was repeated, but the hydrogenationtemperature was controlled to 70° C. The distilled caprolactam wasmeasured, and the results were recorded in Table 1.

Example 3

The caprolactam benzene solution with a concentration of 25.3 wt % wasconcentrated under reduced pressure to obtain a caprolactam benzenesolution with a concentration of 50.1 wt %, and then was fed into thehydrogenation reactor, and the procedure of example 1 was repeated, butthe weight hourly space velocity of the caprolactam benzene solution wasset to 7.55 per hour. The distilled caprolactam was measured, and theresults were recorded in Table 1.

Comparative Example 1

Sodium hydroxide (equivalent to 8 mEq of sodium hydroxide per kg ofcaprolactam benzene solution) was added to the caprolactam benzenesolution with a concentration of 25.3 wt % which was not treated by thehydrogenation, and then the solution was concentrated using reducedpressure machine for the solvent concentration treatment. The lightimpurities were removed by distillation with a vacuum degree of 10 to 15mmHg. Finally, caprolactam was distilled with a high vacuum degree of 3to 10 mmHg. The distilled caprolactam was measured, and the results wererecorded in Table 1.

Comparative Example 2

The caprolactam benzene solution with a concentration of 25.3 wt % wassubjected to a step of water-back-extraction, and the benzene solutionin the aqueous solution was removed by a steam stripping process. Anaqueous solution of caprolactam with a concentration of 39.2 wt % wasobtained.

The caprolactam solution was not subjected to the ion exchange andhydrogenation reaction. The sodium hydroxide (equivalent to 8 mEq sodiumhydroxide per kg of caprolactam solution) was added directly into thecaprolactam benzene solution, and then water was removed asconcentration treatment using the concentrating machine with reducedpressure. The light impurities were removed by distillation with avacuum degree of 10 to 15 mmHg. Finally, the caprolactam was distilledwith a high level of vacuum of 3 to 10 mmHg. The distilled caprolactamwas measured, and the results were recorded in Table 1.

Comparative Example 3

The caprolactam benzene solution with a concentration of 25.3 wt % wassubjected to a step of water-back-extraction, and the benzene solutionin the aqueous solution was removed by the steam stripping process. Anaqueous solution of caprolactam with a concentration of 39.2 wt % wasobtained.

The caprolactam solution was not subjected to the ion exchangetreatment, but it was treated by the hydrogenation. The weight hourlyspace velocity of the caprolactam solution was set to 7.55 per hour.Sodium hydroxide (equivalent to 8 mEq of sodium hydroxide per kg ofcaprolactam solution) was added to the caprolactam solution after thehydrogenation process. Water removing of the concentration treatment wasperformed using the concentrating machine with reduced pressure. Thelight impurities were removed by distillation with a vacuum degree of 10to 15 mmHg. Finally, caprolactam was distilled with a high level ofvacuum of 3 to 10 mmHg. The distilled caprolactam was measured, and theresults were recorded in Table 1.

Measurement

Detection methods used are described below:

Potassium permanganate absorption number (PAN) was measured according toISO 8660. PAN number of caprolactam was a measurement of the amount ofthe impurities which can be oxidized in the caprolactam, and the higherPAN number indicated the presence of a higher amount of impurities whichcan be oxidized.

The measurement of potassium permanganate number (PM)—oxidative capacitywas performed as follows: At 20° C., 3 grams (g) of caprolactam and 1 mLof 0.002 mol/L of potassium permanganate solution were added to 100 mlof pure water, and the time that was required to reduce the colorintensity of the solution to equivalent to the color intensity of thestandard solution was measured, starting from the addition ofcaprolactam and potassium permanganate solution. In which, the standardsolution contained 3000 mg of cobalt nitrate and 12 mg of potassiumdichromate in 1 liter (L) of pure water. The higher PM number indicatedthe presence of smaller amounts of impurities which can be oxidized.

Extinction value was measured according to ISO 7059. Chroma was measuredaccording to ISO 8112.

TABLE 1 Caprolactam analysis of examples 1 to 3 and comparative examples1 to 3 Extinction value PM (sec) PAN (290 nm) Chroma Example 1 320003.13 0.023 <1 Example 2 27000 3.39 0.022 <1 Example 3 35000 2.98 0.026<1 Comparative  5400 11.87 0.077 <1 example 1 Comparative 14000 9.80.068 <1 example 2 Comparative 31000 3.43 0.014 <1 example 3

Based on the results in table 1 for the caprolactam prepared by Examples1 to 3, all PM numbers were more than 20000 seconds, and extinctionvalues (at wavelength of 290 nm) were less than 0.05, PAN numbers wereless than 5, and chroma value was less than 1. All of the resultsindicated the compliance with the quality requirements in the industry.In contrast, the PM numbers of the caprolactam prepared by Comparativeexamples 1 and 2 were less than 20000 seconds, all PAN numbers of thecaprolactam prepared by Comparative examples 1 to 3 were more than thatof Examples 1 to 3, and the extinction values (at 290 nm wavelength) ofthe caprolactam prepared by Comparative examples 1 and 2 were more than0.05. Accordingly, the caprolactams prepared by Comparative examples 1to 3 did not satisfy the industry requirements in term of therequirements for PM number, PAN number and extinction value. Thecaprolactam prepared in Examples 1 to 3 indeed possessed the highquality required in the industry.

In addition, the caprolactam prepared by Example 1 was measured by gaschromatograph (HP6890) with a column of EQUITY™ 701 CUSTOM CAPILLARYCOLUMN (Length 50M×I.D 0.53 μm×film thickness 2.0 μm), a column flowrate of 6.0 ml/min. The column was maintained at a column temperature of80° C. for 8 minutes. Then the temperature was increased to 170° C. withthe incremental rate of 20° C./minute, and the temperature was kept at170° C. for 10 minutes to be analyzed using flame ionization detector(FID) at 250° C. The results do not show the production of cyclohexane,cyclohexene or cyclohexadiene and other substances. Besides simplifyingthe manufacturing process and reducing energy consumption significantly,the present disclosure also enhances the yield and obtains a highquality caprolactam.

It should be noted that all the drawings depict a structure, proportion,size, etc., are only used to indicate the disclosure of thespecification for a person skilled in the art to understand and read. Itis not intended to limit the conditions that can be implemented in thepresent disclosure and thus it does not have substantial technicalmeanings. Any modification of the structure, change of the proportion,or adjustment of the size will be within the scope encompassed in thetechnical contents disclosed in the present disclosure without departingfrom the spirit of the present disclosure.

What is claimed is:
 1. A system for preparing caprolactam, comprising: areaction unit configured to subject cyclohexanone oxime and sulfuricacid to a Beckmann rearrangement reaction to obtain a rearrangementmixture; a neutralization unit connected with the reaction unit andconfigured to receive the rearrangement mixture from the reaction unit,wherein the neutralization unit contains an alkali to perform aneutralization reaction with the rearrangement mixture to obtain a firstcrude caprolactam solution rich in caprolactam and a second crudecaprolactam solution rich in sulfate; an extraction unit connected tothe neutralization unit and configured to receive at least the firstcrude caprolactam solution from the neutralization unit, wherein theextraction unit contains an organic solvent to extract at least thefirst crude caprolactam solution to obtain a caprolactam organicsolution; a hydrogenation unit connected to the extraction unit andconfigured to receive the caprolactam organic solution from theextraction unit, wherein the hydrogenation unit comprises hydrogen and afixed bed, and a hydrogenation catalyst is disposed on the fixed bed tosubject the caprolactam organic solution and hydrogen to a hydrogenationreaction, and wherein a weight hourly space velocity of the caprolactamorganic solution is 1 to 20 per hour, a feeding hydrogen flow rate is0.01 NM³ to 0.15 NM³ per hour per cubic meter of the caprolactam organicsolution, and a hydrogen gauge pressure of an outlet of thehydrogenation reaction is 3 kg/cm² to 20 kg/cm²; and a purification unitconnected to the hydrogenation unit and configured to receive thehydrogenated caprolactam organic solution from the hydrogenation unit,wherein the purification unit comprises an evaporation device and adistillation device.
 2. The system according to claim 1, furthercomprising a first temporary storage unit connected with the extractionunit and the hydrogenation unit, and configured to receive thecaprolactam organic solution from the extraction unit, wherein theelectric conductivity of the caprolactam organic solution is adjusted to5 μmoh/cm to 100 μmoh/cm with an alkali aqueous solution.
 3. The systemaccording to claim 1, further comprising a first concentration unitconnected with the extraction unit and the hydrogenation unit, andconfigured to receive the caprolactam organic solution from theextraction unit, with at least a portion of the organic solvent beingremoved.
 4. The system according to claim 1, further comprising a secondtemporary storage unit and a second concentration unit connected withthe second temporary storage unit, wherein the second temporary storageunit and the second concentration unit are disposed sequentially afterthe extraction unit, and the second concentration unit is connected withthe hydrogenation unit, and wherein the second temporary storage unitreceives the caprolactam organic solution from the extraction unit, andthe electric conductivity of the caprolactam organic solution isadjusted to 5 μmoh/cm to 100 μmoh/cm with an alkali aqueous solution,and wherein the second concentration unit receives the caprolactamorganic solution from the second temporary storage unit, with at least aportion of the organic solvent being removed.
 5. The system according toclaim 1, further comprising a third temporary storage unit connectedwith the hydrogenation unit and the purification unit, and configured toreceive the hydrogenated caprolactam organic solution from thehydrogenation unit, with at least one alkali metal hydroxide added tothe hydrogenated caprolactam organic solution.